Catalysts and process to manufacture 2,3,3,3-tetrafluoropropene

ABSTRACT

Disclosed is a process for the manufacture of 2,3,3,3-tetrafluoropropene comprising: (a) contacting 1,1,1,2,3-pentafluoropropane with a catalyst comprised of chromium (III) oxide having a surface area of at least 150 m 2 /g and having an alkali metal loading of at least 7 milligrams of alkali metal per 100 square meters of catalyst surface area, to produce a product mixture comprising 2,3,3,3-tetrafluoropropene and hydrogen fluoride; and (b) recovering said 2,3,3,3-tetrafluoropropene from the product mixture produced in (a).

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a continuation-in-part of U.S. application Ser. No. 13/188,787, filed Jul. 22, 2011, which is a continuation of U.S. application Ser. No. 12/792,969, filed Jun. 3, 2010, which claims priority to U.S. Provisional application 61/183,674, filed Jun. 3, 2009 and U.S. Provisional application 61/256,341, filed Oct. 30, 2009.

BACKGROUND INFORMATION

1. Field of the Disclosure

This disclosure relates in general to methods of synthesis of fluorinated olefins.

2. Description of the Related Art

The fluorocarbon industry has been working for the past few decades to find replacement refrigerants for the ozone depleting chlorofluorocarbons (CFCs) and hydrochlorofluorocarbons (HCFCs) being phased out as a result of the Montreal Protocol. The solution for many applications has been the commercialization of hydrofluorocarbon (HFC) compounds for use as refrigerants, solvents, fire extinguishing agents, blowing agents and propellants. These new compounds, such as HFC refrigerants, HFC-134a and HFC-125 being the most widely used at this time, have zero ozone depletion potential and thus are not affected by the current regulatory phase-out as a result of the Montreal Protocol.

In addition to ozone depleting concerns, global warming is another environmental concern in many of these applications. Thus, there is a need for compositions that meet both low ozone depletion standards as well as having low global warming potentials. Certain hydrofluoroolefins are believed to meet both goals. Thus there is a need for manufacturing processes that provide halogenated hydrocarbons and fluoroolefins that contain no chlorine that also have a low global warming potential. There is also considerable interest in developing new refrigerants with reduced global warming potential for the mobile air-conditioning market.

HFC-1234yf (CF₃CF═CH₂) and HFC-1234ze (CF₃CH═CHF), both having zero ozone depletion and low global warming potential, have been identified as potential refrigerants. U.S. Patent Publication No. 2006/0106263 A1 discloses the production of HFC-1234yf by a catalytic vapor phase dehydrofluorination of CF₃CF₂CH₃ or CF₃CHFCH₂F, and of HFC-1234ze (mixture of E- and Z-isomers) by a catalytic vapor phase dehydrofluorination of CF₃CH₂CHF₂.

There is a continuing need for more selective and efficient manufacturing processes for the production of HFC-1234yf

SUMMARY

In one aspect, disclosed is a process for the manufacture of 2,3,3,3-tetrafluoropropene comprising: contacting 1,1,1,2,3-pentafluoropropane with a catalyst comprised of chromium (III) oxide having a surface area of at least 150 m²/g and having an alkali metal loading of at least 7 milligrams of alkali metal per 100 square meters of catalyst surface area, to produce a product mixture comprising 2,3,3,3-tetrafluoropropene and hydrogen fluoride; and recovering said 2,3,3,3-tetrafluoropropene from the product mixture produced above.

The foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the invention, as defined in the appended claims.

DETAILED DESCRIPTION

In one aspect, disclosed is a process for the manufacture of 2,3,3,3-tetrafluoropropene comprising: dehydrofluorinating 1,1,1,2,3-pentafluoropropane in the presence of a dehydrofluorination catalyst comprised of chromium (III) oxide, and alkali metal, to produce a product mixture comprising 2,3,3,3-tetrafluoropropene; and recovering said 2,3,3,3-tetrafluoropropene from the product mixture produced in the dehydrofluorination. In one embodiment, the product mixture comprising 2,3,3,3-tetrafluoropropene further comprises less than 20 parts per hundred on a molar basis of 1,1,1,2,2-pentafluoropropane. In another embodiment, the product mixture comprising 2,3,3,3-tetrafluoropropene further comprises less than 10 parts per hundred on a molar basis of 1,1,1,2,2-pentafluoropropane.

In another embodiment, the dehydrofluorination catalyst has a surface area of at least 150 m²/g of catalyst weight and a surface loading of alkali metal of at least 7 mg potassium per 100 square meters of surface area. In another embodiment, the catalyst has a surface area of at least 200 m²/g. In yet another embodiment, the catalyst has an alkali metal loading of at least 8 mg per 100 square meters of surface area. In yet another embodiment, the catalyst has an alkali metal loading of at least 9 mg per 100 square meters of surface area. In another embodiment, the dehydrofluorination catalyst has a surface area of at least 175 m²/g of catalyst weight and a surface loading of alkali metal of at least 9 mg potassium per 100 square meters of surface area. In yet another embodiment, the dehydrofluorination catalyst has a surface area of at least 200 m²/g of catalyst weight and a surface loading of alkali metal of at least 9 mg potassium per 100 square meters of surface area.

Many aspects and embodiments have been described above and are merely exemplary and not limiting. After reading this specification, skilled artisans appreciate that other aspects and embodiments are possible without departing from the scope of the invention.

Other features and benefits of any one or more of the embodiments will be apparent from the following detailed description, and from the claims

Before addressing details of embodiments described below, some terms are defined or clarified.

The catalytic dehydrofluorination of hydrofluorocarbons to produce hydrofluoroolefins is ordinarily carried out in the vapor phase using a dehydrofluorination catalyst. Vapor phase dehydrofluorination catalysts are well known in the art. These catalysts include, but are not limited to, alumina, aluminum fluoride, fluorided alumina, metal compounds on aluminum fluoride, metal compounds on fluorided alumina; chromium oxides, fluorided chromium oxides, and cubic chromium trifluoride; oxides, fluorides, and oxyfluorides of magnesium, zinc and mixtures of magnesium and zinc and/or aluminum; lanthanum oxide and fluorided lanthanum oxide; carbon, acid-washed carbon, activated carbon, three dimensional matrix carbonaceous materials; and metal compounds supported on carbon. The metal compounds are oxides, fluorides, and oxyfluorides of at least one metal selected from the group consisting of sodium, potassium, rubidium, cesium, yttrium, lanthanum, cerium, praseodymium, neodymium, samarium, chromium, iron, cobalt, rhodium, nickel, copper, zinc, and mixtures thereof.

In the preparation of HFC-1234yf by dehydrofluorination of CF₃CHFCH₂F (HFC-245eb), it is possible to obtain either HFC-1234yf or HFC-1234ze, depending on which pair of adjacent fluorine and hydrogen atoms are eliminated. Generally, HFC-1234yf is the predominant product, although depending on reaction conditions, yields of HFC-1234ze can be as much 10 pph or more compared to HFC-1234yf. It has also been found that another by-product of the catalytic dehydrofluorination of CF₃CHFCH₂F (HFC-245eb) is CF₃CF₂CH₃ (HFC-245cb), which can be very difficult to separate from HFC-1234yf. This product is believed to arise via the re-addition of hydrogen fluoride to HFC-1234yf in the direction opposite to that it was eliminated by. Although HFC-245cb can be catalytically dehydrofluorinated to HFC-1234yf, in practice the dehydrofluorination of HFC-245cb requires higher temperatures and a different catalyst. Depending upon the catalyst and reaction conditions, the amount of HFC-245cb produced by isomerization can be as much as from 30 to 60 parts per hundred of HFC-1234yf, resulting in significant yield losses. Selectivity for the production of HFC-1234yf can be expressed as parts per hundred of the by-product relative to the amount of HFC-1234yf. By way of example, a product mixture formed from the dehydrofluorination of HFC-245eb comprising 60% HFC-1234yf, 20% HFC-245cb and 3% HFC-1234ze would have 33 pph HFC-245cb and 5 pph HFC-1234ze.

It is possible to dehydrofluorinate CF₃CHFCH₂F (HFC-245eb) to HFC-1234yf with high selectivity and very little formation of HFC-245cb using a catalyst comprising chromium (III) oxide, and alkaline earth metal. In one embodiment, the alkali metal is one or more of magnesium, calcium, or mixtures thereof.

In one embodiment, the catalyst comprises chromium (III) oxide, and an amount of alkaline earth metal effective to produce 2,3,3,3-tetrafluoro-1-propene while producing less than 20 pph or 1,1,1,2,2-pentafluoropropane. In another embodiment, the catalyst comprises chromium (III) oxide, and an amount of alkaline earth metal effective to produce 2,3,3,3-tetrafluoro-1-propene while producing less than 10 pph or 1,1,1,2,2-pentafluoropropane. In yet another embodiment, the catalyst comprises chromium (III) oxide, and an amount of alkaline earth metal effective to produce 2,3,3,3-tetrafluoro-1-propene while producing less than 5 pph or 1,1,1,2,2-pentafluoropropane. The effective amount of alkaline earth metal required will be dependent upon how it is distributed within the catalyst composition. The effective amount of alkaline earth metal required is also dependent on which alkaline earth metal is chosen. An effective amount of calcium is less than an effective amount of magnesium.

The effective amount of alkaline earth metal required will also depend on the surface area of the catalyst composition. Catalysts which have higher surface areas would be expected to require a higher loading, when described on a weight percent basis, than catalysts with a lower surface area. Another way to express the loading of alkaline earth metal on the catalyst surface which would be independent of changes in amount of catalyst surface area, is to express it as weight of alkaline earth metal per unit catalyst surface area. One example of doing so would be expressed as milligrams of alkaline earth metal per square meter of catalyst surface. Another example would be expressed as milligrams of alkaline earth metal per 100 square meters of catalyst surface.

Unexpectedly, catalysts with high surface areas have different requirements for loading than catalysts with lower surface areas. In one embodiment, the dehydrofluorination catalyst has a surface area of at least 150 m²/g of catalyst weight and a surface loading of alkaline earth metal of at least 7 mg magnesium per 100 square meters of surface area. In another embodiment, the catalyst has a surface area of at least 200 m²/g. In another embodiment, the catalyst has an alkaline earth metal loading of at least 8 mg per 100 square meters of surface area. In yet another embodiment, the catalyst has an alkaline earth metal loading of at least 9 mg per 100 square meters of surface area. In another embodiment, the dehydrofluorination catalyst has a surface area of at least 175 m²/g of catalyst weight and a surface loading of alkaline earth metal of at least 9 mg magnesium per 100 square meters of surface area. In yet another embodiment, the dehydrofluorination catalyst has a surface area of at least 200 m²/g of catalyst weight and a surface loading of alkaline earth metal of at least 9 mg magnesium per 100 square meters of surface area. Catalyst surface area was measured using the BET gas adsorption technique.

In one embodiment, the dehydrofluorination catalyst comprises chromium (III) oxide and at least 1000 ppm alkaline earth metal. In another embodiment, the dehydrofluorination catalyst comprises chromium (III) oxide and at least 3000 ppm alkaline earth metal. In yet another embodiment, the dehydrofluorination catalyst comprises chromium oxide and at least 5000 ppm alkaline earth metal. In yet another embodiment, the dehydrofluorination catalyst comprises chromium oxide and at least 1000 ppm magnesium.

In one embodiment, the dehydrofluorination catalyst may be prepared by slurrying preformed pellets or particles of chromium (III) oxide catalyst in an aqueous solution of an alkaline earth metal salt, such as magnesium chloride or calcium chloride. The slurry is then allowed to dry.

In another embodiment, the dehydrofluorination catalyst may be prepared by slurring chromium (III) oxide powder with an aqueous solution of an alkaline earth metal salt, such as magnesium chloride or calcium chloride. The slurry is then allowed to dry. In one embodiment, the dehydrofluorination catalyst is then pressed, ground into particles, and sieved to 12/20 mesh particles

The physical shape of the catalyst is not critical and may, for example, include pellets, powders or granules.

In one embodiment, the catalytic dehydrofluorination may be suitably conducted with the temperature set point of the reactor in the range of from about 250° C. to about 350° C. In another embodiment, the catalytic dehydrofluorination is conducted with the temperature set point of the reactor in the range of from about 250° C. to about 300° C. In one embodiment, the contact time is typically from about 1 to about 450 seconds. In another embodiment, the contact time is from about 10 to about 120 seconds.

The reaction pressure can be subatmospheric, atmospheric or superatmostpheric. Generally, near atmospheric pressures are preferred. However, the dehydrofluorination can be beneficially run under reduced pressure (i.e., pressures less than one atmosphere).

In one embodiment, the catalytic dehydrofluorination is carried out in the presence of an inert gas such as nitrogen, helium, or argon. The addition of an inert gas can be used to increase the extent of dehydrofluorination. Of note are processes where the mole ratio of inert gas to hydrofluorocarbon undergoing dehydrofluorination is from about 5:1 to about 0.5:1. In one embodiment, nitrogen is the inert gas.

Reaction product HFC-1234yf and any unconverted HFC-245eb are recovered from the effluent leaving the reactor. The unconverted HFC-245eb can be recycled back to the reactor to produce additional HFC-1234yf. In one embodiment of this invention, the unconverted HFC-245eb is recycled back to the reactor as it's azeotrope with HF. Published PCT Application WO 2008/002501 filed Jun. 27, 2006 and, disclosing an azeotrope of HF/HFC-245eb, is incorporated herein in its entirety. U.S. Pat. No. 7,423,188 discloses an azeotrope of the E-isomer of HFC-1234ze and HF and a method to separate the HFC-1234ze from the azeotrope, and U.S. Pat. No. 7,476,771 discloses an azeotrope of HFC-1234yf and HF and a method to separate the HFC-1234yf from the azeotrope. HFC-1234ze may be recovered as a HF/HFC-1234ze azeotrope. Similarly, HFC-1234yf may be recovered as a HF/HFC-1234yf azeotrope. Pure HFC-1234ze and pure HFC-1234yf can be further recovered from their HF azeotropes by using methods similar to those described in U.S. Pat. Nos. 7,423,188 and 7,476,771, and both of which are incorporated herein by reference.

The reactor, or reactor bed, distillation columns, and their associated feed lines, effluent lines, and associated units used in applying the processes of this invention should be constructed of materials resistant to hydrogen fluoride. Typical materials of construction, well-known to the fluorination art, include stainless steels, in particular of the austenitic type, the well-known high nickel alloys, such as Monel™ nickel-copper alloys, Hastelloy™ nickel-based alloys and, Inconel™ nickel-chromium alloys, and copper-clad steel.

As used herein, the terms “comprises,” “comprising,” “includes,” “including,” “has,” “having” or any other variation thereof, are intended to cover a non-exclusive inclusion. For example, a process, method, article, or apparatus that comprises a list of elements is not necessarily limited to only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Further, unless expressly stated to the contrary, “or” refers to an inclusive or and not to an exclusive or. For example, a condition A or B is satisfied by any one of the following: A is true (or present) and B is false (or not present), A is false (or not present) and B is true (or present), and both A and B are true (or present).

Also, use of “a” or “an” are employed to describe elements and components described herein. This is done merely for convenience and to give a general sense of the scope of the invention. This description should be read to include one or at least one and the singular also includes the plural unless it is obvious that it is meant otherwise.

Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Although methods and materials similar or equivalent to those described herein can be used in the practice or testing of embodiments of the present invention, suitable methods and materials are described below. All publications, patent applications, patents, and other references mentioned herein are incorporated by reference in their entirety, unless a particular passage is cited. In case of conflict, the present specification, including definitions, will control. In addition, the materials, methods, and examples are illustrative only and not intended to be limiting.

EXAMPLES

The concepts described herein will be further described in the following examples, which do not limit the scope of the invention described in the claims.

In the examples the follow abbreviations or codes may be used:

-   CT=contact time -   1234yf=CF₃CF═CH₂ -   245eb=CF₃CHFCH₂F -   1234ze=CF₃CH═CHF -   245cb=CF₃CF₂CH₃

Example 1

Example 1 demonstrates the dehydrofluorination of 1,1,1,2,3-pentafluoropropane over a chromium oxide catalyst further comprising boron, potassium and sodium.

An inconel tube (⅝ inch OD) was filled with 6 cc (4.9 gm) of hydrated chromic oxide (also known as Guignet's Green) in extrudate form, which was crushed and sieved to 12/20 mesh. A typical analysis of this catalyst indicated the following composition: 54.5% Cr, 1.43% B, 3400 ppm Na, 120 ppm K. The temperature of the catalyst bed was raised to 325° C. and purged with nitrogen (38 sccm, 6.3×10⁻⁷ m³/sec) for 120 minutes and then at 300° C. for 80 minutes. Then the flow of nitrogen was reduced to 27 sccm (4.5×10⁻⁷ m³/sec) and HF was fed at 9 sccm (1.5×10⁻⁷ m³/sec) for 500 minutes. The flow of nitrogen was then lowered to 19 sccm (3.2×10⁻⁷ m³/sec) and the flow of HF was raised to 15 sccm (2.5×10⁻⁷ m³/sec) for 25 minutes. The flow of nitrogen was then lowered to 11 sccm (1.8×10⁻⁷ m³/sec) and the flow of HF was raised to 21 sccm (3.5×10⁻⁷ m³/sec) for 30 minutes. The flow of nitrogen was then lowered to 4 sccm (6.7×10⁻⁸ m³/sec) and the flow of HF was raised to 27 sccm (4.5×10⁻⁷ m³/sec) for 30 minutes. The flow of nitrogen was then discontinued and the flow of HF was raised to 30 sccm (5.0×10⁻⁷ m³/sec) for 160 minutes. After this activation period, the catalyst bed temperature was changed to reaction conditions.

The reactor temperature was stabilized at temperatures from 250° C. to 302° C., as indicated in the table below, and CF₃CHFCH₂F was fed at 6.4 sccm (1.1×10⁻⁷ m³/sec). The CF₃CHFCH₂F was vaporized at 41° C. while passing nitrogen through the vaporizer at 6.4 sccm (1.1×10⁻⁷ m³/sec). Part of the reactor effluent was passed through a series of valves and analyzed by GCMS. The results in Table 1 are an average of at least two GC injections at each set of conditions. Amounts for 245 cb and 1234ze are expressed as mole parts per hundred of 2,3,3,3-tetrafluoropropene produced.

TABLE 1 Mole % 245cb 1234ze 245eb Temp CT 1234yf (pph) (pph) (%) ° C. (sec) 71.7 8.9 5.2 17.5 302 28 47.9 6.1 4.0 46.6 275 28 28.9 4.5 2.8 68.4 250 28

Example 2

Example 2 demonstrates the dehydrofluorination of 1,1,1,2,3-pentafluoropropane over chromium oxide catalysts further comprising varying amounts of boron, potassium and sodium.

An inconel tube (½ inch OD) was filled with 6 cc (4.9 gm) of hydrated chromic oxide in extrudate form, which was crushed and sieved to 12/20 mesh. Composition of the catalysts with respect to B, Na and K are as indicated in Table 2. The temperature of the catalyst bed was raised to 300° C. and purged with nitrogen (30 cc/min) for 200 minutes. Then the flow of nitrogen was reduced to 60 cc/min and HF was fed at 20 cc/min for 60 minutes. The temperature was increase to 325° C. for 300 minutes. The flow of nitrogen was then lowered to 30 cc/min and the flow of HF was raised to 30 cc/min for 30 minutes. The flow of nitrogen was then lowered to 12 cc/min and the flow of HF was raised to 48 cc/min for 60 minutes. The flow of nitrogen was then discontinued and the flow of HF was raised to 48 cc/min for 30 minutes. The reactor temperature was then decreased to 250° C. for 30 minutes. Afterwards HF was turned off and the reactor was purged with 30 cc/min of nitrogen. The reactor temperature was then stabilized at 300° C., the flow of nitrogen was turned off, and CF₃CHFCH₂F was fed at 3.2 ml/hr (12 cc/min). The CF₃CHFCH₂F was vaporized at 175° C. Part of the reactor effluent was passed through a series of valves and analyzed by GCMS. Amounts for 245 cb and 1234ze are expressed as mole parts per hundred of 2,3,3,3-tetrafluoropropene produced.

TABLE 2 Na K Mole % 245cb 1234ze 245eb Temp CT % B ppm ppm 1234yf (pph) (pph) (%) ° C. (sec) 1.1 3225 135 58.1 28.5 2.7 23.2 300 30 1.6 49 17000 53.7 10.0 2 39.2 300 30 1.6 4550 150 52.8 15.5 2.9 36.7 300 30

Example 3

Example 3 demonstrates the dehydrofluorination of 1,1,1,2,3-pentafluoropropane over chromium oxide catalysts further comprising varying amounts of added potassium.

Chromium oxide catalyst which had a starting composition of 55.8% Cr, 175 ppm Na, 60 ppm K, 53 ppm Cu and 20 ppm Zn was doped with varying levels of potassium. The chrome oxide surface area was 41 m²/g. Composition of the catalysts with respect to amount of K added is indicated in Table 3.

An inconel tube (½ inch OD) was filled with 6 cc (4.9 gm) of catalyst which had been prepared as follows. Hydrated chromic oxide in extrudate form, which was crushed and sieved to 12/20 mesh was doped with varying levels of potassium by slurring catalyst with an aqueous potassium carbonate solution containing enough potassium to provide the indicated potassium levels. The solution was then evaporated to dryness, and the resulting catalyst was dried at 200° C. for 3 hours. After charging the reactor tube, the temperature of the catalyst bed was raised to 300° C. and purged with nitrogen (30 cc/min) for 200 minutes. Then the flow of nitrogen was reduced to 60 cc/min and HF was fed at 20 cc/min for 60 minutes. The temperature was increase to 325° C. for 300 minutes. The flow of nitrogen was then lowered to 30 cc/min and the flow of HF was raised to 30 cc/min for 30 minutes. The flow of nitrogen was then lowered to 12 cc/min and the flow of HF was raised to 48 cc/min for 60 minutes. The flow of nitrogen was then discontinued and the flow of HF was raised to 48 cc/min for 30 minutes. The reactor temperature was then decreased to 250° C. for 30 minutes. Afterwards HF was turned off and the reactor was purged with 30 cc/min of nitrogen. The reactor temperature was then stabilized at 300° C., the flow of nitrogen was turned off, and CF₃CHFCH₂F was fed at 3.2 ml/hr (12 cc/min). The CF₃CHFCH₂F was vaporized at 175° C. Part of the reactor effluent was passed through a series of valves and analyzed by GCMS. Amounts for 245cb and 1234ze are expressed as mole parts per hundred of 2,3,3,3-tetrafluoropropene produced.

TABLE 3 K added - 1234ze 245eb 1234yf 245cb ppm (pph) (%) (%) (pph) 100 13.0 9.73 31.0 45.6 5000 5.30 11.8 73.4 9.5 6500 3.87 34.7 58.6 2.9 10000 0.73 82.4 16.5 0

Example 4

Example 3 demonstrates the dehydrofluorination of 1,1,1,2,3-pentafluoropropane over a gamma alumina dehydrofluorination catalyst.

A batch of gamma alumina (BASF) (6 cc, 3.19 gm) was activated as the catalyst in Example 1 described above. The temperature of the reactor was controlled temperatures from 249° C. to 299° C., as indicated in the table below, and CF₃CHFCH₂F was fed at 6.4 sccm (1.1×10⁻⁷ m³/sec). The CF₃CHFCH₂F was vaporized at 41° C. while passing nitrogen through the vaporizer at 6.4 sccm (1.1×10⁻⁷ m³/sec). Part of the reactor effluent was passed through a series of valves and analyzed by GCMS. The results in Table 4 are an average of at least two GC injections at each set of conditions. Amounts for 245 cb and 1234ze are expressed as mole parts per hundred of 2,3,3,3-tetrafluoropropene produced.

TABLE 4 Mole % 245cb 1234ze 245eb Temp CT 1234yf (pph) (pph) (%) ° C. (sec) 68.7 32.5 8.0 2.9 299 28 64.4 43.3 6.1 3.3 276 28 57.3 46.9 3.3 13.5 249 28

Example 5

Example 5 demonstrates the dehydrofluorination of 1,1,1,2,3-pentafluoropropane over an alpha chromium oxide catalyst.

A batch of alpha chromium oxide (6 cc, 8.51 gm) as described in U.S. Pat. No. 5,036,036 was activated as the catalyst in Example 1 described above. Analysis of the catalyst indicated the following composition: 55.8% Cr, 0% B, 175 ppm Na, 60 ppm K. The temperature of the reactor was controlled temperatures from 249° C. to 298° C., as indicated in the table below, and CF₃CHFCH₂F was fed at 6.4 sccm (1.1×10⁻⁷ m³/sec). The CF₃CHFCH₂F was vaporized at 41° C. while passing nitrogen through the vaporizer at 5.4 sccm (9.5×10⁻⁸ m³/sec). Part of the reactor effluent was passed through a series of valves and analyzed by GCMS. The results in Table 5 are an average of at least two GC injections at each set of conditions. Amounts for 245 cb and 1234ze are expressed as mole parts per hundred of 2,3,3,3-tetrafluoropropene produced.

Analysis of the alpha chromium oxide catalyst indicated it comprised 55.8% chromium, 53 ppm copper, 120 ppm iron, 175 ppm sodium, 60 ppm potassium, 23 ppm manganese, and 20 ppm zinc.

TABLE 5 Mole % 245cb 1234ze 245eb Temp CT 1234yf (pph) (pph) (%) ° C. (sec) 65.5 34.5 11 4.1 298 31 61.8 46.3 8.1 4.1 277 31 57.7 59.4 5.2 4.6 249 31

Example 6

Example 6 demonstrates the dehydrofluorination of 1,1,1,2,3-pentafluoropropane over an chromium oxide gel catalyst.

A batch of chromium oxide gel (6 cc, 7.47 gm) obtained from BASF was activated as the catalyst in Example 1 described above. The temperature of the reactor was controlled temperatures from 249° C. to 298° C., as indicated in the table below, and CF₃CHFCH₂F was fed at 6.4 sccm (1.1×10⁻⁷ m³/sec). The CF₃CHFCH₂F was vaporized at 41° C. while passing nitrogen through the vaporizer at 5.4 sccm (9.5×10⁻⁸ m³/sec). Part of the reactor effluent was passed through a series of valves and analyzed by GCMS. The results in Table 6 are an average of at least two GC injections at each set of conditions. Amounts for 245 cb and 1234ze are expressed as mole parts per hundred of 2,3,3,3-tetrafluoropropene produced.

TABLE 6 Mole % 245cb 1234ze 245eb Temp CT 1234yf (pph) (pph) (%) ° C. (sec) 69.0 33.9 6.4 1.8 299 31 64.4 47.0 4.0 1.5 277 31 59.5 63.4 1.5 0.9 248 31

Example 7

Example 7 demonstrates the dehydrofluorination of 1,1,1,2,3-pentafluoropropane over a chromium oxide gel catalyst.

A batch of chromium oxide gel (6 cc, 5.9 gm) obtained from Synetix (CPA200A) was activated as the catalyst in Example 1 described above. The temperature of the reactor was controlled temperatures from 251° C. to 301° C., as indicated in the table below, and CF₃CHFCH₂F was fed at 6.4 sccm (1.1×10⁻⁷ m³/sec). The CF₃CHFCH₂F was vaporized at 41° C. while passing nitrogen through the vaporizer at 5.4 sccm (9.5×10⁻⁸ m³/sec). Part of the reactor effluent was passed through a series of valves and analyzed by GCMS. The results in Table 7 are an average of at least two GC injections at each set of conditions. Amounts for 245 cb and 1234ze are expressed as mole parts per hundred of 2,3,3,3-tetrafluoropropene produced.

Analysis of the chromium oxide gel catalyst indicated it comprised 62.9% chromium, 350 ppm copper, 198 ppm sodium, 145 ppm iron and 50 ppm potassium.

TABLE 7 Mole % 245cb 1234ze 245eb Temp CT 1234yf (pph) (pph) (%) ° C. (sec) 70.8 30.5 6.2 1.8 301 31 65.9 43.6 3.9 1.5 276 31 67.3 42.6 1.9 1.3 251 31

Example 8

Example 8 demonstrates the dehydrofluorination of 1,1,1,2,3-pentafluoropropane over a chromium oxide catalyst doped with varying levels of potassium with a surface area of 213 m²/g. Potassium loadings on the catalyst are expressed as mg potassium per 100 m² of catalyst surface area.

A batch of chromium oxide (6 cc, 7.47 gm) obtained from BASF was doped with potassium and activated as the catalyst in Example 3 described above. The temperature of the reactor was controlled temperatures from 250° C. to 300° C., as indicated in the table below, and CF₃CHFCH₂F was fed at 6.4 sccm (1.1×10⁻⁷ m³/sec). The CF₃CHFCH₂F was vaporized at 41° C. while passing nitrogen through the vaporizer at 5.4 sccm (9.5×10⁻⁸ m³/sec). Part of the reactor effluent was passed through a series of valves and analyzed by GCMS. The results in Table 8 are an average of at least two GC injections at each set of conditions. Amounts for 245 cb are expressed as mole parts per hundred of 2,3,3,3-tetrafluoropropene produced.

TABLE 8 % K Temp added K (mg/100 m²) % 1234yf pph 245cb % 245eb (° C.) 0.65% 3.1 38.3 154 0 250 34.6 171 0.42 275 39.6 134 0.64 300 1.0 4.7 44.6 45.7 32.1 250 51.7 68.9 8.26 275 52.6 73.7 0.65 300 1.5 7.0 59.0 16.1 28.5 250 69.2 26.2 8.27 275 72.2 26.2 0.56 300 2.0 9.4 32.7 3.1 65.2 250 57.7 5.4 37.0 275 70.6 6.6 21.4 300 2.5 11.7 18.9 0.95 80.0 250 43.2 2.7 53.6 275 65.9 4.0 28.4 300

Example 9

Example 9 demonstrates the dehydrofluorination of 1,1,1,2,3-pentafluoropropane over a chromium oxide catalyst doped with varying levels of potassium with a surface area of from 44 to 125 m²/g. Potassium loadings on the catalyst are expressed as mg potassium per 100 m² of catalyst surface area.

A batches of chromium oxide (6 cc, 7.47 gm) having surface areas of 44 m²/g, 125 m²/g or 130 m²/g were doped with potassium and activated as the catalyst in Example 3 described above. The temperature of the reactor was controlled at temperatures from 250° C. to 351° C., as indicated in the table below, and CF₃CHFCH₂F was fed at 6.4 sccm (1.1×10⁻⁷ m³/sec). The CF₃CHFCH₂F was vaporized at 41° C. while passing nitrogen through the vaporizer at 5.4 sccm (9.5×10⁻⁸ m³/sec). Part of the reactor effluent was passed through a series of valves and analyzed by GCMS. The results in Table 9 are an average of at least two GC injections at each set of conditions. Amounts for 245 cb are expressed as mole parts per hundred of 2,3,3,3-tetrafluoropropene produced.

TABLE 9 Surface % K K (mg/100 area % pph % Temp added m²) (m²/g) 1234yf 245cb 245eb (° C.) 0 0 44 42.8 4.9 51.0 250 0 0 44 66.9 11.0 19.6 275 0 0 44 71.5 19.4 5.49 300 0.1 2.3 44 21.5 1.1 77.0 250 0.1 2.3 44 44.1 4.3 50.7 275 0.1 2.3 44 65.2 5.7 24.7 300 0.2 4.5 44 18.3 0.7 80.6 250 0.2 4.5 44 36.6 1.6 60.5 275 0.2 4.5 44 60.4 3.2 32.7 300 0.3 6.8 44 21.8 0.6 76.4 275 0.3 6.8 44 23.5 0.6 74.3 300 0.3 6.8 44 44.3 0.7 50.5 325 0.3 6.8 44 52.2 0.7 40.2 351 0 0 125 20.4 3.0 78.4 251 0 0 125 42.0 6.3 53.7 275 0 0 125 62.2 9.6 27.4 300 0.1 0.8 125 9.9 1.1 89.5 250 0.1 0.8 125 18.8 1.3 79.9 275 0.1 0.8 125 34.3 1.8 62.9 300 0.1 0.8 125 45.5 2.0 50.2 325 0.1 0.8 125 55.2 1.8 39.1 350 0 0 130 47.3 97.9 1.28 250 0 0 130 46.8 102 0 275 0 0 130 59.0 57.5 0 300 0.1 0.8 130 32.6 5.14 64.6 250 0.1 0.8 130 58.0 10.0 33.6 275 0.1 0.8 130 73.4 16.1 10.1 300 0.2 1.54 130 10.2 0.43 89.2 250 0.2 1.54 130 22.9 0.80 75.6 276 0.2 1.54 130 42.1 1.23 54.5 300

Note that not all of the activities described above in the general description or the examples are required, that a portion of a specific activity may not be required, and that one or more further activities may be performed in addition to those described. Still further, the order in which activities are listed are not necessarily the order in which they are performed.

In the foregoing specification, the concepts have been described with reference to specific embodiments. However, one of ordinary skill in the art appreciates that various modifications and changes can be made without departing from the scope of the invention as set forth in the claims below. Accordingly, the specification and figures are to be regarded in an illustrative rather than a restrictive sense, and all such modifications are intended to be included within the scope of invention.

Benefits, other advantages, and solutions to problems have been described above with regard to specific embodiments. However, the benefits, advantages, solutions to problems, and any feature(s) that may cause any benefit, advantage, or solution to occur or become more pronounced are not to be construed as a critical, required, or essential feature of any or all the claims.

It is to be appreciated that certain features are, for clarity, described herein in the context of separate embodiments, may also be provided in combination in a single embodiment. Conversely, various features that are, for brevity, described in the context of a single embodiment, may also be provided separately or in any subcombination. Further, reference to values stated in ranges include each and every value within that range. 

What is claimed is:
 1. A process for the manufacture of 2,3,3,3-tetrafluoropropene comprising: (a) contacting 1,1,1,2,3-pentafluoropropane with a catalyst comprised of chromium (III) oxide having a surface area of at least 150 m²/g and having an alkali metal loading of at least 7 milligrams of alkali metal per 100 square meters of catalyst surface area, to produce a product mixture comprising 2,3,3,3-tetrafluoropropene and hydrogen fluoride; and (b) recovering said 2,3,3,3-tetrafluoropropene from the product mixture produced in (a).
 2. The process of claim 1, wherein said alkali metal is potassium.
 3. A process of claim 1, wherein said product mixture comprising 2,3,3,3-tetrafluoropropene comprises less than 20 parts per hundred on a molar basis of 1,1,1,2,2-pentafluoropropane.
 4. The process of claim 1, wherein said product mixture comprising 2,3,3,3-tetrafluoropropene comprises less than 10 parts per hundred on a molar basis of 1,1,1,2,2-pentafluoropropane.
 5. The process of claim 1, wherein the catalyst has a surface area of at least 200 m²/g.
 6. The process of claim 1, wherein the catalyst has an alkali metal loading of at least 8 milligrams of alkali metal per 100 square meters of catalyst surface area.
 7. The process of claim 1, wherein the catalyst has an alkali metal loading of at least 9 milligrams of alkali metal per 100 square meters of catalyst surface area.
 8. The process of claim 1, wherein the temperature of the catalyst is maintained at a set point of from 250° C. to 350° C.
 9. The process of claim 6, wherein the temperature of the catalyst is maintained at a set point of from 250° C. to 300° C. 